Method for producing ammonium phosphate



Fig.4. 4,

July 24, 1951 0.-R |cE 2,561,415

METHOD FOR PRODUCING AMMONIUM PHOSPHATE Filed June 25, 1948 e Sheets-Sheet 1 ag 3% -W July 24, 1951 0. RICE 2,561,415

IMETHOD FOR PRODUCING AMMONIUM PHOSPHATE Filed June 23, 1948 6 Sheets-Sheet 5 INVENTOR Owe/2 Pica.

# ATTORNEY July 24, 1951 RICE 2,561,415

METHOD FOR PRODUCING AMMONIUM PHOSPHATE Filed June 23, 1948 6 Sheets-Sheet 4 INVENTOR 123" 122 Owe/2 Pz'ce 1Z3 BY gl/td-zd 5 -G x fl- ATTORNEY July 24, 1951 0, RICE 2,561,415

METHOD FOR PRODUCING AMMONIUM PHOSPHATE Filed June 2a, 1948- G'Sheets-Shet 5 INVENTOR 7C 0 a)? Fake.

BY #4 ATTORNEY July 24, 1951 0. RICE 2,561,415

METHOD FOR PRODUCING AMMONIUM PHOSPHATE Filed June 23, 1948 6 Sheets-Sheet 6 4&4 J2. Jga

' lNVENTOR er? Pz'ce BY 1 fi ATTORNEY Patented July 24, 1951 METHOD FOR PRODUCING AMMONIUM PHOSPHATE Owen Rice, Bridgeville, Pa., assignor to Hall Laboratories, Inc., a corporation of Pennsylvania Application June 23, 1948, Serial No. 34,789

16 Claims. 1

This invention relates to processes for the manufacture of ammonium phosphate having a composition corresponding substantially to the formula NH4PO3, as determined by analysis.

An object of this invention is to produce an ammonium phosphate in a dry micro-crystalline powder form which is non-hygroscopic under the temperature and atmospheric conditions encountered in storage in the various climates.

A further object of the invention is to produce 7 a product of the type referred to above having a composition corresponding substantially to the formula NH4PO3 as determined by analysis and a definite X-ray diffraction pattern characterizing the product as a crystalline chemical compound.

A still further object of the invention is to provide a new and novel process for the production of ammonium phosphate as a dry, crystalline powder by reacting gaseous phosphorus pentoxide produced by burning elemental phosphorus with atmospheric air, and ammonia gas and cooling the gaseous-reaction product at such a rate that the ammonium phosphate produced is a dry crystalline powder and collectible on filters.

, A still further object of the invention is to ef' feet the reaction of NH3 gas, atmospheric air containing water vapor, and gaseous phosphorus pentoxide whilethe reactants are in a gaseous phase and at such a temperature that the amu monium phosphate product is produced, and then cooling the gaseous-reaction product at such a rate that it may be collected on filters without plugging the same. Phosphorus which has been burned to phosphorus pentoxide is believed to be a polymer of P205 at the temperatures at which it exists as a gas. For convenience, this form of the phosphorus pentoxide also will be referred to herein as (P2O5)w where :r is an unknown, be lieved to be 2.

'In carrying out one form of the process embodying this invention, elemental phosphorus in a' molten condition is supplied to a combustion or reactionchamber to which atmospheric air containing water vapor for burning the phosphorus to phosphorus pent/oxide and ammonia gas are supplied. The ammonia gas may also be reacted with the '(P2O5)m at a point removed from the combustion or flame zone of the phosphorus provided the temperature of the (P205):c and excess air containing moisture is high enough for the gaseous phase reaction to take place and produce the crystalline ammonium phosphate in the collectible form.

-"'I'-h-e-atmospheric air, which contains water vapor, is supplied to the combustion zone at a rate in excess of the rate theoretically required to burn elemental phosphorus to (Prom. There appears to be no limit to the amount of excess air that may be supplied insofar as successful performance of the process is concerned. However, as will be pointed out later in this specification, a minimum excess exists below which an ammonium phosphate product that is collectible on filter surfaces, cannot be produced.

The gaseous ammonia that is supplied to react with the water vapor in the combustion air and the gaseous phosphorus pentoxide is also fed at a rate in excess of the amount theoretically required to produce NH4PO3. The ammonium phosphate produced in the combustion or flame zone, or at a point outside the flame zone where the ammonia gas is introduced into the gaseous (P2099; in a zone removed from the flame zone, I prefer to call a gaseous-reaction ammonium phosphate product.

I have discovered that ammonium phosphate produced by the reaction of water vapor, gaseous (P20s)a:, and NH3 gas, must be quickly cooled from the gaseous state in order that the product may be rendered collectible on filters. If this gaseous-reaction product is allowed to remain at a high temperature for more than a few seconds, it decomposes to a sticky, viscous, and highly hygroscopic substance having a glassy or amorphous character. Such a product will clog the filter surfaces almost instantly and require the process to be shut down until clean filters can be substituted. Furthermore, such a product is useless for commercial purposes because it cannot be packaged or handled.

The gaseous reaction should be carried out at temperatures below about 900 F. as ammonia burns at about this temperature. The amount of excess air for a given rate of burning of phosphorus should be so adjusted that the temperature in the reaction zone does not exceed that at which ammonia burns or decomposes. The reaction product should be cooled rapidly after it has formed so that it may be collected as a dry crystalline ammonium phosphate.

Quick cooling of the gas-reaction ammonium phosphate product may be effected in several ways, for example by supplying large excesses of atmospheric air; by supplying a large excess of air and introducing liquid water, as a mist or spray, into the air; or by utilizing a large excess of air and passing the mixture of the unreacted air water vapor and NH3 gas, and the gaseousreaction product which is suspended in such mixture through a heat exchanger, which may either be air or water cooled, and thence through a filter where the product is collected. If the cooling of the gaseous-reaction product has been rapid enough, the product will collect on the filter surfaces without plugging them. If the product has not been cooled quickly enough and the glassy, sticky, hygroscopic product above" described is formed, the. filters willplug almost instantly. If: a suflicient excess of NH3 is supplied in relation to the rate at which the elemental phosphorus is being burned, and a non-collectible product is formed, it is quite certain that the rate of cooling. the gaseous-reaction product is too low. This can be corrected by increasingthe amount.- of ex-. cess air provided the cooling.:capacity...available from excess air or from a combination vor" excess air and a heat exchanger are adequate. The precautions to be observed in so operating the process that a collectible ammonium phosphate may be produced, are relativelysimple and arc-readily. determinable.

If the process. is. to be carried out by reacting all of the reactants in a combustion space and passing the reaction products through a heat exchanger and a filter on which the ammonium phosphate product is collected, a given rate of phosphorus feed is first decided upon. This rate would ordinarily be much lower than the estimated capacity of the equipment in which the. process is. to be carried out. The amount of air theoretically required to burn this amount of phosphorus is then calculated. The rate at which the air is to be supplied would then be increased to a value of say 20 to 30 times the calculated theoretical value. The rate at which NI-Ia gas is to be supplied would also be substantially in excess of the theoretical amount required to form the product NH4POs-say 200% of theoretical. Provision should also be made for measuring the temperature of the mixture of excess air, NI-Is gas,.water vapor and ammonium phosphate carried in suspension in such mixture just before it enters the filter.

When these calculations have been made, the air and-NHQ are supplied tothe combustion zone, after which the phosphorus feed is started. The phcsphoru'sjburns spontaneously and generates. heat at a rate of about 11,200 E. t. u. per pound.

Under these conditions the gaseous-reaction product produced is cooled rapidlyby reason of the huge excess of. air and the cooling effect of the heat exchanger, and is collectible on the filters. The rate of feed of phosphorus is then. gradually increased, the rate of feed of ammonia gas being adjusted along with it to maintain a. predetermined excess, say 200% of theoretical, and the temperature of the reaction product ahead of the filters is noted. The phosphorus input may be graduallyincreased to a value where'a non-collectible product isformed, a con dition that immediately becomes known through the plugging of the filter surfaces. When plugging conditions are first noticed, the temperature should be noted, the process stopped and clean filters substituted for the plugged ones. The process may then be started up again, the rate of feed of phosphorus being decreased to a value where the temperature of the reaction product.

and the unreacted' mixture of air and NH3 enter-' ing the filters is safely below that at which plugging had previously occurred. The cost of operating the process depends in part on the amount of excess NHs used. Therefore, no more than is necessary to form .a collectible productshould be used. To find the minimum excess rate of NH:

for the maximum phosphorus feed that has been determined as above described, the ammonia feed rate may be gradually reduced. While the ammonia feed is being reduced, the temperature of the mixture entering the filters should be noted, and the first signs of filter plugging should be watched for; When signs of. plugging of the filters. appear, theammonia feed rate should be noted as this may be the minimum excess permitted. The ammonia feed rate should then be increased to a safe value above the minimum so determined, to assure trouble-free operation.

The theoretical amounts by weight of ammonia (NI-ls) and elemental phosphorus required to produce 'onepoundaof ammonium metaphosphate is in the. ratio of about 1'? to 31, the necessary amount cf'water'being assumed. In other words, for every 31 pounds of phosphorus, i7 pounds of ammonia (N53) are theoretically required, I propose to use. an excess of ammonia, but at-the same timeemploy as small an excess .as can be.

used and still producea satisfactory product that.

can be collected on filters without plugging them.

Theratio of ammonia to phosphorus may vary from say about 0.65:1 to about 2:1, and in prac-.

tice the ratio may be maintainedbetween.about.

1.25:1 to about 2:1 on a weight basis.

In the above description, it has been assumed that when the phosphoruswas burned at maximum rate, the cooling. capacity of the'system had been utilized fully. Tlius, by observing the filters and rates of feed of phosphorus and ammonia, that rate of cooling of the gaseous-reaction reference should be had to the accompanying.

drawings in which:

Figure I-is a more or less diagrammatic view of the experimental apparatus that was employed in determining the conditions of operation under. which'a gaseous-reaction product of ammonium phosphate could be. produced by reacting am mon'ia with the fumes of burning phosphoru'sflin the flame zone thereof, and the water'vap'or present in" atmospheric air whichwa's suppliedlfor' the combustion" of phosphorus andrapidly'cooling the gaseous reaction product, the. resulting product being: one whichcculd be collected" on":

filter surfaces without plugging the same Fig. 2 isya top plan viewof the filter arrange-i ment' forithe apparatus shown in" Fig. l;'

Fig. dis a more or less diagrammatic view of. a modified form-of apparatus wherein the'am" introduced into the" gaseous" (P2095: at a pointremovedfrom the flame zone. in order that conditions for the production of a" collectible product by gas-phase reaction-could monia gas was be determined.

Fig. 4- is a top plan view'of the filter apparatus of Fig.3; 7

Figs; 5 and 6 are graphsshowing rates of cooling'of gaseous-reaction"product of" ammonia, air

containing moisture, and gaseous P205 at which a dry, crystalline ammonium-phosphate powder form may be produced in'collectible form on.

filter surfaces.- without pluggingthe same;

Figs. 7a, 7b, and 7c are views in side elevation, par tly in-section, of sectionspqf apparatus for carrying out the process on a commercial scale, these views when placed end to end representing the complete diagrammatic arrangement of the apparatus;

Figs. 8a, 8b, and 8c are top plan views of the apparatus shown in Figs. 7a, 7b, and 7c respectively.

Fig. 9 is an end view of the phosphorus burner shown in Fig. 719;

Fig. is a view in section taken on lines X-X of Fig. 9;

Fig. 11 is a view partly in section of a modified form of product collecting apparatus; and

. Fig. 12 is a view in section taken on line XII-XII of Fig. 11.

Throughout the drawings and the specification, like reference characters indicate like parts.

In Fig. 1 the apparatus illustrated with which ammonium phosphate of the ammonium metaphosphate composition was produced on an experimental basis in accordance with the invention, comprises a reactor I, a discharge conduit 2, and a filter system 3. The reactor I was made from a metal drum having an inside diameter of approximately 22 inches and a length of approximately 3 feet. The elemental phosphorus was supplied through a pipe 4 to the interior of the forward end of the reactor drum from a receptacle 5, such as a glass jar. The phosphorus receptacle 5 was placed in a tank 6 and covered with water. The jar 5 in which the elemental phosphorus was contained was also filled with water. The water in tank 6 was heated by a gas burner I to a temperature at which elemental phosphorus was in a molten condition, so that when pressure was applied to the interior of jar 5, the phosphorus would flow to the reactor.

The elemental phosphorus was caused to flow out of the jar or bottle 5 by means of a constant head siphon 8 which supplied water to the jar vor bottle 5 at a fixed but regulated rate. The air for burning the phosphorus was supplied by means of a fan or blower 9. This fan discharged the air into the reactor drum at its forward end. "The ammonia gas was introduced into the suction of the fan from a steel cylinder In containing ammonia under pressure. The fiow of ammonia from the cylinder was regulated by means of a regulating valve II. The rate at which air was delivered to the reactor chamber and the rate at which ammonia gas was delivered to the suction of the fan was measured by means of orifices and manometers. The discharge conduit for the fan was provided with an orifice I2 and a manometer I3 measured the pressure drop across that orifice. The pipe leading from the ammonia cylinder to the suction pipe of fan 9 was provided with an orifice I4, and the pressure drop across it was measured by a water manometer I5. By means of the manometers I3 and I5, the rates at which ammonia and air were supplied to the reactor were determined.

In order that the pressures obtained in the reactor chamber could be ascertained, a water manometer I6 having a pressure connection I! with the interior of the reactor was provided.

This manometer registered changes in pressure thermometer [8 was mounted in the drum at a.

99??? e e t W m t removed 1 m the flame of the burning phosphorus, a shield being employed to keep radiation of the flame away from the. thermometer.

During the performance of some of the experiments, the only cooling medium for the gaseousreaction product of ammonia, gaseous (.PzOah, and water vapor, was the excess air supplied by fan 9. By excess air is meant the excess of air over and above that theoretically required to burn elemental phosphorus to (P205)=. In other experiments, additional cooling of the gaseousreaction product was effected by means of a water-cooled coil I9 disposed within the drum at a distance of about eighteen inches from the center of the flame zone of the burning phosphorus.

The filter system 3 comprised a pair of ducts 2| and 22 disposed at an angle of about 45 to each other to which filter bags 23 and 24 were connected. These filter bags were made of cotton duck cloth. The lower ends of these bags were open but were held closed during operation by means of clamps 25.

The process was commenced by starting the blower or fan 9, following which the ammonia was turned on, so that a mixture of ammonia gas and air was flowing through the reactor into the filter bags. The phosphorus feed was then started and as soon as the molten phosphorus reached the combustion chamber, it spontaneously burst into flame. The ammonia gas, the (P205) :1: formed by the burning of the phosphorus, and the water vapor in the combustion air reacted to form, in the gaseous phase, a gaseousreaction product, crystalline ammonium phosphate having a composition corresponding to NI-I4PO3.- The amount of air supplied was varied from what might be regarded as a relatively small excess to a huge excess with reference to the amount of phosphorus that was being supplied to the reaction chamber during any particular experimental run. The ammonia supply was varied also from what might be regarded as a slight or small excess over and above the theoretical required to produce ammonium metaphosphate, NH4PO3, to a relatively large excess of the order of several hundred percent.

In experimenting with the process, blower 9 was operated to deliver its maximum volume of air and the ammonia was adjusted in relation to the rate of feed of phosphorus. For example, for a given feed of phosphorus, the ammonia would be adjusted to a value that would be in excess of that required to produce a product corresponding to the formula NHrPOa. With the air adjusted to full volume, the phosphorus was fed to the combustion chamber, first at very low rates. The reaction product was collected on the filter bags. The product collected was a dry white crystalline powder.

The rate of feed of phosphorus was then gradually increased and the temperature in the combustion chamber as measured by the thermom eter I8 was observed. As the rate of phosphorus feed was increased, the B. t. u.s generated increased proportionately which resulted in ever increasing temperatures in the reactor drum I. It was found that when the temperature in the reactor became too high, the gaseous-reaction product produced would be a sticky, syrupy, glass-like substance which would almost immediately plug the filter bags so that the process would have to be shut down and the bags washed to render them serviceable again. The sticky substance. resulted because cooling fromthe high temperature. phase to a temperature at which 73' the-:reaction-prccluct is sable; could: notwbe eitfectedrrapidiy. enough; Cooling. must be accome plished at the required rate not onlytoproduce a i stable collectible productzbut also ato protect thevfilter bags against charringpandirburning. Cooling, in-.the reaction Z0118 .is alsonecessarygto prevent development of temperatures '1 atwhich ammonia burns.v Ammonia burns-:or decomposes at temperatures.slightly'above 900F;

By. supplying air, ammonia. gas; and. phosphorus to this experimental device at various. rates, data were. obtained from which. the curves in' Flgs;::,5 and d were ploted. Curves 20 in these graphs were plottedfrom data obtained from-manygtrial The ordinates of thesercurves represent the. temperature as measured by thermometer l8, and the abscissae represent the time in which'the gaseous-reaction product was cooled from agiventemperature. These curves show that so longer the gaseous-reaction product of ammonia, burning phosphorus, and water vapor, arew'cooled at a rate such that the time-temperaturev relation ship during, cooling is maintained to the left. of thecurve, a product that was collectible. on the filter bags could be produced. HOWGVGIZlf the time-temperature relationshipswere such as to fall in the area to the right of the curves, a noncollectible product was obtained which plugged the filter bags almost instantly.

As is exident from Fig. 2, the product produced could be shunted'to one or the other of the filter bags by means of a damper 30. Thuswhenever.v it was-necessary-to empty a bag; the gaseous-reaction product was alldiverted to onebagwhile the other was emptied, and vice versa. The. bags wereemptied as freqeuntly as necessary to maini tain the pressure in the combustion chambertat a reasonably low value so as not tocut down'thevolume of air delivered by the blower.

Referring again to the curves in Figs. 5 and 6,- the following will indicate the necessityfor -ob-- serving the temperature cooling-rate relationship.

of the gaseous-reaction product.

In Fig. 5 are represented the cooling rates'per missible for producing a product that can be collected on the filter bags without pluggingthem;

when the temperature in the reaction zone as measured by thermometer is is maintainedat about 600 F. If the reaction product'ismaine tainedin the reactor at 800 F. for moreathanl about 4.6 seconds, the product decomposes, plug.- ging the bags.

When sufficient water vapor has beentaken up in exchange for the ammonia .so released;;the1 product becomes a glass-like substance WhiChiTlS very sticky and hygroscopic. Such a pro-ductal most instantly plugs the filter bags; IfJthe gasthat represented by cooling-rate line 30.

As may be seen by inspection of Fig; 5,. coolingrate line 30 lies on curve ZF'thI'OLlQhOUGltS- The angle .a between .this line straight portion. 30 and a perpendicular dropped from-the 4.6:sec-

onds point on'the curve represents an'angle'with in. which the cooling-rate line.mayfallltol-prm duce a collectible product.

Apparently when the gaseous-' reaction product is held at this temperature for" this period of time or longer, ammonia is released from the product and replaced by water vapor.:

If thecooling-rateline falls outside of this angle andtothe right of line 30, a non-collectible product. :is obtained; If. theparticles of ammonium phosphate-taxes maintained at a: temperature. of. 600 Estonia-1 shorter-attimea say 3.8: seconds, the coolingsrate angle iisrrepresented- Joy c1. The. lowest .cooli'nge ratelineforangleal isdesignated by numeral 31..- This line also is tangent to the curve .285 If-Ltha gaseousereaction: product remains at about.v 600 "forsaboute seconds,thelcoo1ing=rate maybe at a rate not less than that indicated by line 3 l',..and atany. highe-r=rate .representediby a linelwithin angle :11. When the cooling rate .is withinthis angle, .aicollectible..product .is obtained. Iflthe gaseous-reaction product is maintained ata'rtemperature of 60.0?v F. for a. period-of about; 21seconds, the cooling-rate line angle :isthatYdeSige. natedtas :1 and the cooling rate should benotless than about that indicated by line. :32.

Thezcoolingeratesxof the gaseousereacti on product .ar'exdepende'nt. on: thevolume :ofiexcess supplied-to the chamber in which the reaction occurs; Iniother words, the greaterthe volumezof.

airisupplied; the greater will be the volumeiand; velocity :of air passinglthrough' the-reactor :to :the'

filtersbagsy themair containing. the. gase'ousereac tion product; thepexcess aininonia' and the excess waterwvapor which is. co-ntainedin the air sup-ipliedit'o-the reactor.

In .Fig-.. 6;the graph. illustrates the cooling rate where-the maximumanieasured temperatureinthe combustion-chamber of the. reactor is; approx.- imately; 500 F; Whenwthe temperature-is not permitted to exceed about 500 the gaseous;

reaction productcan remain at this temperature for-a maximum period of about between. sixand seven seconds before it begins to decompose i or change to the glassy, sticky substance whichscan not-beicollecterl on the-filter bags. To :avoidzdecomposition: under these-conditions the cooling rate requiredshould be not less than. the: rate indicated bygcurveit, and the coolingerate angle designated-.ibyrangle a. If thegaseous-reactionx product is maintained at aztemp'erature of 5.0091

for: a. period-sofabout'four seconds, the lowest coolihgrateeat which :a: collectible. productcan be producedis that-indicatedby cooling-rate line; and: :the cooling-rate angle .is :12. The cooling.-

r rate; lilies.- represented by a2 and c1: are both tangent to curve 28%- but at diiferent points' thereon.

Ol'wthefcu-IVes shown in Figs. 5 audit, it is apparent that. "the higher the temperaturemaint'ained in the reaction zone, the more rapidly the gaseous-reacticn product must becooled, and; that when the gaseous-reaction product is maintainedtata-given temperature for shorter periods of time. thepro'duct may be cooled-at lower rates.

From the experiments conducted with-the experimental apparatus shown in Figs. 1 and '2; I

found that a gaseous-reaction product couldbe produced satisfactorily at a temperature in the combustion" chamber up to about 900 F. How'- ever, I prefer to carry out the process under con-.

ditlons where the maximum temperature'inithe combustion; chamber should not. exceed .900

nor be substantially below. 600 F.. Ammonia burnsflor decomposes at a temperature lslightlyg H above-900 FE, therefore temperatures thatihigh should be avoided. Of course, the higher the temperature that can be safely. maintained in the. cornbustion'chamberfor a given installation hay ing agiven maximum coolingcapacity; the more" heat can be transferred by heat exchange to water cooled surfaces so that the additional cooling required' can be effected by" employing excess air. Since heatexchangefor cooling purposes more efficient at thehig'her 'tei'nperatures h'igher phosphorusburning ratesmaybe practiced? The more phosphorus that can be burned in any given apparatus, the higher the rate of production will lie for that apparatus.

The apparatus shown in Fig. 1 was first oper *ated without any heat exchanger such as represented by cooling coil i9. After the maximum capacity of the apparatus had been reached with air cooling, the cooling coil was inserted within the drum and water circulated through it. The temperatures of the water at the inlet and outlet of this cooling coil were measured to determine the B. t. u. transferred to the cooling water. By utilizing the heat exchanger, it was possible to increase the feed of phosphorus and still produce an ammonium phosphate product that was collectible on the filter bags without plugging them.

In Fig. 3, a cylindrical drum 4!) was mounted ahead of reactor drum l of Fig. 1 and the phosphorus was burned in this drum. Drum 4|] was about 20 inches inside diameter and about four feet long. The outlet of this drum was connected by a pipe 4! to the front end of drum 1. The filter system was modified so that a larger num ber of filter bags could be used and at the same time make discharge of the phosphate product into containers more convenient.

The filter system employed in Fig. 3 comprised a U-bend 42 which was connected to the outlet of the second drum (drum I) and this U-bend discharged into a hopper 43. The top of the hopper was provided with six bags 4d made of cotton canvas-duck. The bottom of the hopper was provided with a chute from which the prodnot was discharged into drums. The product that was collected on the bags was removed from the bags by shaking as frequently as necessary to prevent the back pressure on blower 8 from building up too high.

The elemental phosphorus was introduced through a pipe into drum 4!!! by the same feeding arrangement that is shown in Fig. 1.

A baffle 46 was mounted inside drum 48 to the :right of the phosphorus feed pipe so as to provide a combustion chamber 41. The blower 9 was mounted to discharge the air into the combustion chamber, and ammonia was delivered to the intake of the fan in the same manner as shown in Fig. 1. The heat exchanger IQ of Fig. l was employed in the second drum as shown in Fig. 3, and additional cooling was provided by means of a spray pipe 41 which sprayed water over the drum 4!] and pipe 4|. With this arrangement, more cooling capacity was provided so that phosphorus could be burned at a higher rate in the apparatus and still produce the ammonium phos=- phate product that was collectible in the filter bags without plugging them.

In another experiment, the ammonia was reacted with the burning phosphorus with the gaseous (P205)r at a point outside the immediate flame zone. Ammonia was introduced by pipe 48 into the outlet end of drum Gil at the point where the gaseous (P205)? entered pipe 4!. It was found that so long as the gaseous (P205) 11: was maintained at a sufficiently high temperature, the ammonia and the gaseous (PzOsM would react to form an ammonium phosphate product of the same quality and kind as was produced in the apparatus shown in Fig. 1. In order that a collectible ammonium phosphate product may be produced under these conditions, the temperature of the (P205) :1: should not be below about 600 for otherwise when the ammonia is introduced into the gaseous (P2091, a sticky non-collectible product is likely to result. .So long as the (P2093:

10 is hot enough to be in gaseous form rather than in what appears to be a phosphoric acid state, the reaction which results in a collectible product will take place.

It was observed by temperature measurement that when the ammonia reacted with the gaseous (P2091, there was substantial heat of reaction observed in order to obtain a collectible ammonium phosphate product were readily de terminable from the character of the end product. These limiting conditions can be determined by following the operating steps suggested below for the type of reaction illustrated in Fig. 1. First, one would supply to the apparatus all the air that the blower could supply. Second, the ammonia should be introduced into the air stream in quantity greatly in excess of that required to react with the (PzOsM to form the ammonium phosphate product which analyzes according to the formula NHaPOc. Next, the phosphorus feed is turned on and the temperature was measured at the point where the gaseous-reaction product, excess air, and excess ammonia in which it would be suspended, enters the filter system. If the product resulting is collectible on the filter bags, the phosphorus feed is increased, and if a collectible product results, the phosphorus feed is again increased. By continuing the increase of the phosphorus feed in small increments, a point will finally be reached where a non-collectible product will be produced. This point was reached when cooling of the reaction product was not accomplished rapidly enough. The deficiency in cooling occurred because the capacity for cooling had been exceeded. When a non-collectible product was produced and the bags plugged, the temperature at which that condition occurred and the rate of feed of phosphorus at that moment were observed. When plugging occurred, operation of the process was stopped. After cleaning the bags so as to render them operable, the process was started up, but the phosphorus feed was kept below that rate at which the plugging had occurred in the previous run. This could readily be determined by observing the temperature in the drum and keeping the rate of feed of phosphorus at a value where the plugging temperature would not be reached.

When the ammonia is introduced into the gaseous (P2093.- as described in connection with Fig. 3, the phosphorus feed and the amount of excess air should be so adjusted as to develop such a temperature at the point of ammonia addition, that the (F209;: will be in a gaseous rather than in a phosphoric acid state, a collectible ammonium phosphate product may be produced. The temperature of the gaseous (P205)a: can be measured and by adjusting the phosphorus feed and the amount of excess air, a desired temperature can be maintained at the point where the ammonia is added. Also the temperature of theair laden product at the en trance to the filter system should be measured to determine whether the rate of cooling the am-,

monium phosphate product is sufficient and also to protect the filter bags against burning or charring. When the relationships of the reactants air, moisture in the air, ammonia and gaseous I111 -(B205) Ja -which result .in-.-a collectible :a-mmonium phosphate product, .havebeen determined; the process is on an operating basis.

In the operation of the processsuchasabove described, the plugging condition .is "a useful zin- .dicator. 'It is useful-because it not.:only.:de

tor-mines whether too much phosphorus is being burned for. the cooling capacityofthe system, but. whether the amount "of ammonia supplied ,is too low, or whether ornot too much water vapor has been introduced into .the-reactants'forthe gaseous-reaction, product.

In the experiments periormed-by-the apparatus .shoWni-nFigs. l and 3., I also introduced into? the .air.-.supply, liquid water'as-a mist, in addition to introducing water in addition; to that. contained in the air, a considerable cooling chest: is: obtained which increases the 'coolingi-capacitywof thesystem. .This added water may be Supplied by: spraying it into the air stream-ahead-of .the combustion chamber or it may be sprayedaqinto the combustion chamber.

Fromthe dataobtained by the experimental apparatus shown in Figs. 1 and 3, apparatus, such as that indicated :by Figs. 7a to '10 inclusive, and 8a tor-8c inclusive, was designed for-carrying out the precessflona larger scale.

-In Figs. 7a, 7b, and *Zcand the corresponding topgxplan views 8:1,8-12; and--80, I have illustrated tanks and 52 for storing elemental phosphorus, a fire xtube boiler 53 in which. the elemental phosphorusisburned and rea'cted with ammonia, gas, and Water vapor contained in .ythe'zzcombustion air, land a-filter system 54. :in. whichthe ammonium phosphate product is collected.

The phosphorusstorage tanks 5lvandw52 are mounted inca pit 55 ofsuch.'depthnand volume that'if by accident eitherorboth storagetanks should leak, theelemental phosphorus lwould. be trapped the pit and covered .vvith themwater that is-alwaysmaintainedin the pit. :Storage tanks 5! and 52 are so 'arrangedvthatwhile phosphorus is being-supplied toathexreactor-Bfi from one of these-tanks; thezother tankrcanzb'e refilled with, phosphorusdireotly froms'a' :tan'k car 56.

.Eachcf the storage tanks .51 and: His provided witha heating coil 5'! through which hot-Water is circulated to :maintain the phosphorus'iin' a molten condition.

Asis shown :more clearl in-Figs-8a, tanksi 5|:

and '52 are provided with a .header- 5 8, the"gopposite -ends of which are. connected to pipes 5'9 and {50 that extend downwardly through the top of thetanks to points near the bottoms thereof.

A T 6| is provided in the header to which a-pip'e 62 isconnected that supplies phosphorus to the combustion chamber of the reactoriii. :Pipe 62 is disposed in a housingv 63 throughwhich. hot

water flows to maintain theaphosphorus in the domes -67 and'68 respectively. Riserpipes 69 charge end near the'bottom of the car.

and; 'likextend through these" domes anddown- *wardly. into, the. tank and their upper. endsaare car 55-when2the-same is being unloaded.

rHe'aderl-i zisiprovidedwithva'lves M and i5 disposed-on opposite sides of T 12, so 'thatby :closing one .of them and opening the other, phosphorusmay be unloaded into either tank 5| critank 52'.

The tank car. 56 is' provided with the customary :heating. cells 18 through which hot water or steamis: passed to heat andmelt the phosphorus so that it may .be displaced by water and caused tofiow therefromfinto' the storage tanks. An unloadingpipe' so extends through dome 8! of the carcand downwardly'into the same with its dis- The upperend ofithis'pipe is connected by a valve 32 tofithexphosphorus unloading pipe E3. The water used to forcethe phosphorus out of the tank car into zthe'unloading pipe "l3 enters the dome" 8! through. a valve 83. This water is forced into thewtankicar from one or the other of the tanks 5! and 52, whichever is to be filled with elemental phosphorus, through a pipe 85. Pipe is connectedxto arcs and a header 8?, the opposite .ends'of which are connected toriser pipes wand 9 that communicate with the interior of tanks 4 and. 52 respectively.

*Valves Elfi and Marc provided in headers! ontopposite sides of T 86 so that by closing one oftthese valves and opening'the other, phosphorus be caused to flow to one or the other of tanks 5] and: 52. A pump 92 may be provided in a bypass 93 associated with riser pipe 88, a valve 94 being provided in the riser so that'when it is closed, the pump will pump water out of tank 5! and *into the tank car 56 to initiate flow of phosphorus from the tank car into tank 5!. 'It is to be noted that if tank 5! has been emptied of phosphorusand is to be refilled, that the tank will be full of water. As this water is pumped into"-the' tank car, phosphorus will flow out of it into v:tank'5i. When this how has started, valve 9 may beopened to permit siphoning action to unload phosphorus from the car into tank-5| A similar-pump by-pass and valve may be provided in riser 89 to be usedwhen tank52 isto be'filled withiphosphorus.

Ta'nks 5| and 52 may be provided. with standpipes Shandy! respectively, in which the water level'may be'carried at predetermined heights depending upon the rate at which it is desired to feed phosphorus from the storage tanks to the reactor 53. Gauge glasses Y 98 and Eli? may be provided for indicating the head of water on each of these tanks.

In order to facilitate controlling the pressure head of Water in either phosphorus tank 5| or 52,the"standpipes 9t and 9? are each provided with a plurality of overflow valves ldfla, It'iib, l flllcrespectively. If any one of these valves is opened,"the others being closed, water is introduced into the tanks, the waterlevel will rise until it flows out the open valve. If the flow of water into the tanks is adjusted to" equal the ammmtoverflowing through the open valve, the pressure head on the phosphorus will be constant.

Water for displacing phosphorus in the storage tanks is introduced through supply pipes liilla and Hill) respectively, having valves I92 and 11.03 therein lfOI' adjusting the rate of flow or 13 waterin the tanks. The supply pipes Ilila and Hill) may be extended to the reactor 53 or some other convenient point with the valves I52 and I03 located at such points so that the water level in the tanks 54 and 52 may be conveniently adjusted.

The water employed for heating the phosphorus in the tank car 55 is supplied from the reactor 53 when the process is in operation. Water enters the water space of the reactor from a supply pipe I04 and the hot water is discharged therefrom through a pipe Hi5. The amount of heat generated by the burning of the phosphorus and the reaction between the phos phorus fumes and the ammonia, under ordinary conditions, is sufiicient to supply the hot water necessary for operation of the process. Hot Water from the reactor is also directed into housing 63 by a pipe I55 to keep the phosphorus in the feed pipe 52 in a fluid condition.

As shown in Figs. 7a, and 82), pipe m5 is connected by a pipe Ill! to a lateral Hit the opposite ends of which are connected to the heating coils in the storage tanks 5| and 52. Valves I99 and I I are provided in the lateral so that hot water can be delivered to either or both of the heatin coils 51. Pipe I also supplies the heating coil 18 in the tank car being connected thereto by a pipe III in which a valve H2 is provided.

The water passing through the heating coils of tanks 5! and 52 and of car 56 discharges into pit 55 and a drain H3 respectively, the drain also taking the overflow from the pit.

It will be. observed by inspection of Figs. 7a to 70 inclusive that the phosphorus storage tanks are mounted at a lower level than the fire box N5 of the reactor 53, so that in case of a shutdown of the plant, or in case a break occurs in the phosphorus feed pipe 62, the phosphorus will flow back into the storage tank, or if any escapes from the feed pipes, the same will flow into the pit 55 where it will sink and be covered with water and rendered harmless from the standpoint of fire or spontaneous burning in the air.

The reactor 53 may comprise a fire tube boiler because of its relatively simple construction. The size of this boiler in terms of rating, such as boiler horse power capacity, may be as large or as small as desired. The capacity of boiler selected for the apparatus shown in the drawings was approximately an 80 horse power. This boiler was modified by scaling up the fire box so as to provide a tight combustion chamber. II5.

Air for burning the phosphorus may be sup" plied by a plurality of blowers (not shown) through what would be the fire door of the boiler by means of a conduit H6.

The ammonia required in the process is stored in a storage tank IIB from which it is delivered to the reactor through a feed pipe I I9. In order that the ammonia may be thoroughly mixed with the air delivered to the reactor chamber II5, the discharge end of the ammonia feed pipe I I9 is disposed in pipe I I6.

The phosphorus feed pipe 62 delivers the phosphorus to a burner I20 in the reactor cham her I I5.

Burner I29 comprises a tunnel I2I of refrac tory material having side walls I22 which support the tunnel in spaced relation to the fioor or house of chamber H5. The vertical run I23 of the phosphorus feed pipe 62 is disposed at one side and to the rear of the tunnel. The upper end of run I23 is bent horizontally and then down- 14 wardly with the discharge end of the pipe extending'through the roof of the tunnel.

To provide primarily air for the phosphorus, a pipe I24 is provided. One end of this pipe projects into the air pipe H5 and the opposite end extends into the tunnel and is so positioned that air is directed at the tip of the phosphorus pipe that extends into the tunnel. In order to regulate or adjust the flowof air through pipe I24, a damper I25 is placed in the discharge end of air supply pipe IIE. Damper I25 may be positioned by an operator I26 such as an air cylinder, for example.

The total flow of air both secondary, (the air which passes damper I25) and primary air may be adjusted by a damper I2'I and a damper operator I 28 such as a power cylinder, for example. In order that the rate of flow of phosphorus to combustion chamber IE5 may be regulated, a diaphragm operated valve I29 is provided in phosphorus feed pipe 62. This valve is operated by pressure such as compressed air supplied from a supply pipe I3Il. The particular value of pressure supplied to the diaphragm chamber of valve I25 is under the control of a hand sender or regulator I 3| such as disclosed in U. S. Patent No. 2,304,782. While the regulator may be of the type shown in this patent, any suitable pressure sending device may be employed. The rate of flow of phosphorus through the pipe 62 may be determined by a meter such as an indicating manometer I32 that measures the pressure drop across an orifice I33 in the feed pipe. The pressure differential as measured by this meter is a measure of the flow of phosphorus.

The rate of flow of ammonia to the combustion chamber may be regulated by means of a diaphragm operated valve I35 disposed in the ammonia feed pipe H9. The pressure supplied to the diaphragm chamber of this valve may also be derived from the pressure sent out by the sender I3I through the sending line I35. In order that the rate of flow of ammonia with respectto the rate of flow of phosphorus may be adjusted so that the ratio of the rate of how of one to the other may be varied as required in the operation of the process, a ratio relay I36 is interposed between the sending line I35 and the diaphragm chamber of the valve I34. The ratio relay I36 receives pressure from line I35 and depending on the adjustment of the relay I36, this relay transmits a loading pressure to the diaphragm chamber of valve I34 through a line I31. The pressure sent out through line I3? is derived from a supply source I38 such as compressed air. The ratio relay indicated may be of the type shown in U. S. Patent No. 2,304,783. While I have indicated a ratio relay of the type shown in this patent, it is to be understood that any relay which will provide a ratio of any desired but predetermined value between the loading pressures transmitted to the diaphragms of valves I34 and I29 according to the requirements of the process, may be employed.

In order that the rate of flow of ammonia through pipe I I9 to the combustion chamber may be determined, a meter may be provided that measures the pressure drop across an orifice MI in pipe I I9. The meter may be of the manometer type such as indicated at M2. When an operator is operating the process, he judges the relative rates of flow of ammonia and phosphorus by observing the readings on the manometers I42 and I32 respectively.

When the process is in operation, the secondary and primary air beingsupp'lied "to fthe-ifurnac'e as above described and the phosphorus being delivered to the burner I 20, the phosphorus burns vigorously and forms a gaseous phosphoruspentoxide. The ammonia which is introduced with the air and the water vapor contained in the air react with this gaseous phosphorus pentoxide to formammonium phosphate which is crystalline in form and has by analysis a composition corresponding to NHiPOa. In the-combustion chamber, the reaction product'resulting is at ahigh temperature depending on the amount of excess-'air-that is supplied. The rate at which phosphorus is burned in "the combustion chamber and the amount of excess air supplied are so adjusted that the temperature in this chamber will not reach the value at which ammonia burns or decomposes. Ammonia decomposes or burns at temperatures slightly above 900 F. and it is therefore necessary to stay below this temperature. The reaction product formed in the combustion chamber passes through the fire tubes I43 of the first pass to'asmoke box I44 from which it enters abank of fire tubes I45 of the secondpass into the outlet smoke box I41 of the'iurnace. The reaction product formed in the combustion chamber is cooled partially by radiant heat given up to the fire box walls which are-water cooled and a substantial amount of this heat is given up to water surrounding the fire tubes I45 in the'first pass. As-"the product-passesthrough the second'pass consisting of the fire tubes I46, it is further cooled. The amount of excess air supplied also takes up a large part of the heat and effects coolingof the product.

In operating the process, I prefer to'measure the temperature in the smoke box I44 and in the smoke-box I41 so that it maybe ascertained whether or not the reaction product has been cooled quickly enough to prevent decomposition of" the product into the sticky glassy-like substance heretofore described. "The temperature maybe measured in the smoke box I44 by means of a thermometer, either an indicating or recordi-ng thermometer such as indicatedat I48. 'The temperature in the outlet smoke box I41 maybe measured by a thermometer MB. This thermometer may be either an indicating or arecording thermometer. The reaction product leaves the smoke box I41 through one or the other of pipes or conduits I56 and 15!. Pipe I56 supplies units I52 and I55 of the filter'system 54 while pipe 'I5I supplies unit I55 and I55-respectively thereof. As shownin Fig. 8c, uni-ts I52 and I53 are connected'by a pipe I55, and units I54 and I55 are connected by a pipe I51.

-When' the ammonium phosphate reactionproduct is delivered to units I52 and 153-01 the filter system; a damper I56 in pipe .II is closed sothat theraccumulation ofproduct in units I54 and I 55 may be unloaded or "removed fromjthefiltering elements. Likewise, when product i supplied through pipe I5! to units I54 and I55.a damper I.59, in-pipe I50 is closed so thattheproduct acoumulatedinthe filter elements of units 152 and I 53.may be dislodged therefrom.

The. filter units I 52 through I55 inclusive are similarin construction; therefore, only unit-I53 need be described as this is illustrated quite plainly ,in Fig. 7c. The filter unit I 53 comprises ahopper ISO-made of sheet metal or other suitable material which. is pressuretight so asto avoid leakage of the fine ammonium phosphate reaction product delivered-to it. Thetop of the, hoppengisclosed ammonium metaphosphate,

by a suitable cover plate I6I whichis formed a plurality of openings each having a vertical flange I62 associated therewith and to which the lower end of a filter such as a filter bag I63 may be secured by means of a clamp I64 (see Fig. 12). Filter bags I63 may be made of cloth or fabric of suitable material. I have found that cotton duck is a suitable material for the filter bags as is nylon also. Both of these materials are resistant to the temperatures encountered and are durable. The nylon material appears to be more durable than cotton, but eithernylon or cotton'is suitable for thepurpose.

As illustrated in Figs. 7c and 80, each of the units I52 through I55 inclusiv includes about 48 filter bags. The number of filter bags employed per unit will depend on the permeability of the filter bag material and the total amount of product that has to be filtered.

The upper ends of the filter bags may be con nected to a support member I65 suspended from links I66 in such manner that the support mem-- ber I65 may be oscillated. The mechanism for oscillating the support member I65 may be of any suitable form or type. As illustrated schematically, the mechanism may include a crank arm I61 that is connected to one end of the support member I55. One arm of the crank isconnected to a diaphragm operator I68 towhichpressure may be applied intermittently to provide a downstroke that turns crank I61 clockwise, the return 01 up-stroke being accomplished by a compression spring I69. This up and down motion of the diaphragm is transmitted through a push rod I16 to the bell crank and results in" an oscillatory'motion of the support member I65 with a corresponding motion of the bags.

As is well understood in this art, bags of this type can not be shaken when pressure is on'them. Therefore, when the bags of the pairs of units I52-J 53 and I54--I 55 are to be shaken, the pressure to them is out off. Thus, for example, if the bags of units I52 I53 are to be shaken, the damper in pipe I55 is closed and the-interior of the hoppers I60 of units I52-I53 and the bags are connected to atmosphereby means of a pipe I12 to-which, if desired, an exhaust fan I13 may be connected to insure that there will be no tension on the bags because of pressure. A damper I14 is provided in pipe I12 so that when thebags of units I52I53 are to beshaken, and damper I50 has been closed as aforesaid, the damper 114 is moved to open position and fan I13 exhausts air from the bags and'hoppers of units I52-I53. Thus, whenthe shaker operator IE8 is supplied with intermittent pressure, the bagswill be deflected back and forth 'with the motion of the support I65 and any material adhering to them will be dislodged and fall into the hoppers.

When the bags of units I54-I55 are to :be shaken, damper I12 in pipe I14 is closed, damper I59 is opened, and damper I58 in pipe I.5I is closed. When the damper I 58 is closed, a damper I14 provided in a pipe I12 communicating with the interior of pipe I5I is opened so that-a fan I13 may exhaust the bags and the hoppers associated with units I'54--I55, thereby to relieve these units of pressure from within, and permitting the bags to befiexed by th shaker operator. As may be seen from Figs. 7c andSc, I have illustrated a shaking mechanism only for the unit I5,3,;but it {is to be understood thateach of the units I52, I54, and I55 is providedwithsimilar shaking units. and operated as aboveadescribed whennecessary to freethe .bagsof the ammonium 1? phosphate reaction product that may be adhering'to the inner surfaces thereof.

The material falling into and collecting in the hoppers I60 discharges into a conveyor I extending centrally under all of them. This conveyor may be of any suitable type such as a screw conveyor and driven by a motor I8I. Conveyor I80 delivers the phosphate product to a conveyor I82 driven by a motor I83 whereby the product is carried to an elevator I84. Elevator driven by a motor I85 and carries the product to'a hopper I06 from which itmay be discharged at thebottom thereof into bags or other containers for shipment or storage.

The apparatus employed for removing the product from the hoppers I60 of the filter units may of course be materially different in design from that schematically illustrated in the drawings. This matter i largely a question of choice and selection dictated-by the needs of a particular plant.

In the arrangement shown in Figs. 7a'7c, and

Figs. 811-80, the air supplied for combustion of the phosphorus, cooling the ammonium phosphate product, and conveying it to the filter units, isall supplied by forced draft fans located ahead of the reactor 53. In other words, the system is under pressure. It may be desirable to use both pressure and vacuumonthe system to make the system more flexible and to facilitate control of pressures in the reaction chamber H5. To use'both pressure and vacuum, i. e. forced and induced draft on the system, I may modify the filter 'system shown in Figs. 7c and 8c in the manner indicated in Fig. 11. Q In Fig. 11, the filter bags of each filter unit are enclosed in a pressure tight housing I88 connected to an exhaust or induced draft fan I89. Fan I89 reduces the pressure on the outside of the filter bags and assists in drawing the ammonium phosphate reaction product andthe excess air in which it is suspended through the reactor, the intervening piping, and the bags. By adjusting the induced draft operating on the housings of the filter bags in relation to the air supplied by the forced draft fans to the combustion chamber of the reactor, the pressure in the. reaction chamber of the reactor and at points between. the reactor and the filter system may be adjusted.

As shown in Fig. 11, the bags of each filter unit may be shaken to remove the product that adheres to the .innersurfaces thereof, by means ofxa diaphragm unit I98 mounted on the top of the housing. These units are so arranged that their respective diaphragms I90 are connested-to. the bag support members I by push rods. I9I. When pressure is applied to the diaphragm chambers, the push rods move downwardly and are returned by compression springs I92 when the pressureis released. By applying pressure intermittently to these diaphragm chambers, bags IE3 are flexed and shaken.

The flexing of the bags is accomplisched when the pressure on the unit has been cut off as by closing one or the other of dampers I50 and I5I closing damper I94 at the suction side of fan I99,. and opening a flapper valve I93 in a pipe I94 connected to the intake of the exhaust fan whereby the pressure inside and utside the bags is equalized at atmospheric. Thus, when the pressure is removed from the filter bags, they are flexible. and in condition for flexing and shaking bythe shaker-diaphragm operators I68.

The 'processuforxmaking ammonium phosphate I84 is '18 above described may be started up and carried on in various ways but the following procedure is suggested:

l. The phosphorous in the storage tank should be heated up to a temperature of about 150-170" F. to insure that the phosphorus is molten and in a fluid condition. This can be accomplished by circulating hot water through the heating coils in the tank. Until the proc ess has been started up and hot water is'available from the reactor, the necessary hot water can be supplied from an auxiliary heater (not shown).

2. The water in the reactor should also be heated up as by circulating hot water through it from an auxiliary heater.

3. The forced draft fans are started up and adjusted to supply say 200 or more percent of air in excess of that required theoretically to burn the phosphorus at the rate it will be supplied to the reactor chamber.

4. Either damper I50 or I5I leading to the filter unit is closed while the other is held open depending on which filter unit is to be put in operation first.

5. Ammonia is turned on, by opening valve I34; at a rate that will provide an excess over the requirements for the production of ammonium metaphosphate, NHiPOg, say excess based on the rate atwhich the phosphorus will be fed to the burner of the reactor.

6. Water is run into the phosphorus storage tank until the desired pressure head on the phosphorus is obtained.

7. The phosphorus control valve I29 in the feed line 62 is opened by supplying pressureto the diaphragm thereof, the valve being opened only a little at first. When thephosphorus flows into the burner, it burns spontaneously.

8. The phosphorus feed valve is then opened gradually to increase the rate of burning.

9. The temperatures indicated by thermometers I48 and I49 are observed.

10. The phosphorus feed rate may be increased until the maximum temperature desired in the outlet smoke box I4! is reachd. This temperature should not exceed 400-475 F.

Whenthe maximum phosphorus feed rate has been reached, the ratio relay I36 is adjusted until the ammonia feed has been reduced to a minimum excess over the theoretical requirement for-the reaction to result in NI-I4PO3, say about 25% of excess. After this relay has'been adjusted, adjustments in the rate of feed if both phosphorus and ammonia may be made simultaneously without disturbing the desired ratio of ammonia to phosphorus by merely turning the hand wheel of the sender relay I3I.

When a given rate of operation has been reached, the temperature at the outlet smoke box M! can be controlled by adjusting the secondary air supplied to either increase or decrease the excess of air. The more excess air supplied, the more the reaction product is cooled, with consequent reduction in temperature in both of smoke boxes I44 and I4 1. The temperature in smoke box I44 should always be below 900 F. and ought not to exceed 650 F. If this temperature is exceeded, the probabilities are that the temperature in the combustion or reaction chamber will be so high as to cause burning or decomposition of the ammonia.

During starting up and running of the process, the condition of the phosphate product should be observed. If a glassy sticky product Iii fsufiicient ammonia is being supplied to the reaction chamber. By adjusting the rates of air, ammonia, and phosphorus supplied to the reactor until the proper cooling rates are achieved and a collectible product is obtained, operating conditions can be established for a continuous operating process that will result in a collectible ammonium phosphate product being formed.

If the air is too dry and not enough moisture is available for the reaction to produce NHiPOs, moisture may be added as steam or as a mist or spray to the air supply duct I I6. This process will function with large excesses of water in the reaction chamber and the excess does not appear tobe critical with respect to successful operation of the process. However, the process is critical with respect to deficient moisture, so care should be taken to insure that the minimum theoretical amount of water is available in the reaction chamber to allow complete reaction to take place between the water, phosphorus pentoxide, and ammonia.

,Also, in operating the process, the temperature cooling rate data indicated by the curves in Figs. and 6 should be followed as this data indicates the. rate at which the ammonium phosphate product, once it has been formed, must be cooled from a high temperature down to a temperature at which the product is stable with respect to atmospheric conditions. While the upper temperature limits indicated in Figs. 5 and 6 are in the neighborhood of 600 F. it is to be understood that the temperature maybe carried upwardly to near 900 F. provided cooling is accomplished rapidly enough with excess air and supplementary heat exchange.

The filter units should be alternated in the collection of the product. Shaking of the bag filters vshouldbe done as often as necessary. If the pressure inthe combustion space in thereactor rises to a value above a maximum desired value or the total flow of air decreases, that is an indication that the bags are becoming too impervious to the flow of air and require shaking. 'I'he'alternating. shakin of the bags may be done on a scheduled cycle, if that is desired, so that each bag will be shaken every few minutes, say every four or five minutes. Operation of the processwill indicate whether more or less frequent shaking is necessary.

. From the foregoing it will be apparent to those skilled in this particular art that various modifications and changes may be made in the practice of the process without departing either from the spirit or the scope of the invention. Therefore, what I claim and desire to secure by Letters Patent is: v 1. A method of producing ammonium metaphosphate as a dry free-flowing powder that consists insupplying air containing moisture and elemental phosphorus to a combustion chamber at such ratios relative to each other that the phosphorus is burned to gaseous phosphorus pentoxide and supplying the phosphorus and air to said combustion chamber at such rates that the temperature developed in said chamber by said combustion is above 600 F., introducing ammonia into the phosphorus pentoxide formed said chamber and the water vapor mixed therewith in such amounts that the ammonia and water vapor react with all the gaseous phos phorus pentoxide to form ammonium metaphosphate while the reactants 'are in the gas phase, continuously discharging the excess airand ammonium metaphosphate so formed into a filter, and cooling the ammonium meta-phosphate and air at such a rate that the temperature thereof is reduced from the temperature at which the metaphosphate is formed in the gas phase to a temperature in the filter at which the ammonium metaphosphate remains stable as a dry free flowing powder; in a cooling time period not ex-' ceeding 8 seconds.

2. A method according to claim 1 characterized by the fact that the ammonia gas is supplied at a rate in excess of the amount theoret'-' ically required to produce NH4PO3 and the air is supplied at a rate substantially in excess of the amount theoretically required to burn ele-' mental phosphorus to phosphorus pentoxide to efiect cooling of theammonium metaphosphate gaseous-reaction product, and, prior to filtering, passing the air laden with NH4PO3 through a heat exchanger to cool the air and thereby further cool the particles of NH4PO3 suspended therein.

3. A method according to claim 1 characterized by the fact that coolin of the gaseous reaction product is eifected by supplying atmospheric air to the combustion chamber at a rate greatly in excess of the rate theoretically required to burn elemental phosphorus to phosphorus pentoxide at the rate at which it is fed to the combustion chamber.

4. A'method according to claim 1 characterized by the fact that the ammonium phosphate reaction product and the excess air and ammo nia are conducted from the combustion chamber through a heat exchanger to further cool the ammonium phosphate reaction product prior to filtering.

5. A method according to claim 1 characterized by the fact that cooling of the gaseous reaction product is efiected by supplying atmospheric air to combustion chamber at a rate greatly in excess of the rate theoretically required to burn elemental phosphorus to phosphorus pentoxide at the rate at which it is fed to the combustion chamber, and that prior to filtering, conducting the excess air and ammonia and the phosphate reaction productsuspended therein, through a heat exchanger.

6. A method of producing a dry, crystalline ammonium phosphate having a ratio of (NH-QzQ to P205 of about 1:1, which comprises feeding elemental phosphorus to a combustion zone, supplying atmospheric air to said zone at a rate at" least equal to 300% in excess of the theoretical air required to burn the phosphorus to phos phorus pentoxide, supplying to said'zone concomitantly with the supply of air, ammonia gas in amount not less than about 30% in excess of the amount theoretically required to form NH4P03, causing said excess air and ammonia containing the said reaction product, to fiow to a filter in which the reaction product is collected and separated from said air andexcess am monia gas, and so regulating the rates of feed of phosphorusand air relative to one another that the temperature of the reaction product is reduced from the temperature existing at the combustion zone to a value of about 400 F'at the filter in such a period of time that the "re-- action productdoes not change from a dry 'p'ow- 21 1 der to a sticky glass-like mass which adheres to and plugs the filter surfaces of the filter.

7. A method of producing a dry, crystalline ammonium phosphate having a composition corresponding essentially to NH4PO3 which comprises feeding phosphorus to a combustion zone, supplying atmospheric air to said zone at a rate at least equal to 300% in excess of the theoretical ,air required to burn phosphorus to phosphorus pentoxide, supplying to said zone concomitantly with the supply of air, ammonia gas. at a rate not less than about 30% in excess of the amount theoretically required to form NH4PO3, passing the gaseous reaction product and theexcess air and ammonia in which it is suspended through a heat exchanger wherein the air and ammonia are cooled thereby cooling the particies of ammonium phosphate suspended therein, causing said ammonia and the reaction product and excess air to flow from said heat exchanger to a, filter in which the reaction prodnot is collected and separated from said air and ammonia, and so regulating the relative rates of feed of phosphorus and air that the temperature of the reaction product is reduced from the te1nperature existing at the combustion zone to a value of about 400 F. at the filter in such a period of time that the reaction product does not change from a dry powder to a sticky glasslike-inass which would adhere to and plug the filter surfaces of the filter.

.- 8. The method of producing ammonium phosphate as adry crystalline powder, which comprises feeding elemental phosphorus to a combustion zone, supplying atmospheric air containing water and ammonia gas to said zone to form while in a gas phase, a reaction product of ammonia, water vapor, and phosphoruspentoxide, the air bein supplied at a rate equal to at least 300% of the theoretical amount of air required to burn phosphorus to phosphorus pentoxide, the ammonia being supplied at a rate equal to at least 30% in excess of the amount required to form with the gaseous phosphorus pentoxide a product having a composition corresponding sub stantially to that of NHiPOg, passing said ammoniurn phosphate reaction product while in suspension in said excess air to a collector containing air pervious filter surfaces, measuring the temperature of the air and gas stream with its entrained ammonium phosphate at a point adjacent the collector, varying the cooling rate of said ammonium metaphosphate by adjusting the rate of feed of phosphorus relative to the rate of supply of air until the said phosphate converts to a sticky glass-like material and plugs the filter surfaces of said collector, observing the temperature of the phosphate and air entering said collector at which said conversion occurs, and so regulating the relative rates of supply of phosphorus and air to said chamber that the temperature of the air and phosphate product entering said collector is below the value at which plugging of the filter surfaces occurs.

9. A method according to claim 8 characterized by the fact that the air supply is maintained at a value between about 150% to 1000% in excess of the theoretical amount of air required to burn phosphorus to phosphorus pentoxide, that a ratio between the rate of feed of ammonia gas and phosphorus is maintained at between about 1.25:1 to about 2:1 on a weight basis, and that the rate of feed of phosphorus is so regulated that the temperature of the air and ammonia gas containing therein the ammonium 22 phosphate in suspension, as it leaves the heat exchanger, is below the value at which the ammonium phosphate decomposes to a sticky glassflre product.

10. The method of producing ammonium phosphate as a dry crystalline powder, which comprises feeding elemental phosphorus t a combustion zone, supplying atmospheric'air and ammonia gas to said zone to form while in a gaseous phase, a reaction product of ammonia, water vapor, andphosphorus pentoxide the air bein supplied at a rate equal to at least 300% of. the theoretical amount of air required to burn phosphorus to phosphorus pentoxide, the ammonia being supplied at a rate equal to at least 30% in excess of the amount required to form with the gaseous phosphorus pentoxide, a producthaving a composition corresponding essentially to that of NH4PO3, passing the gaseous ammonium phosphate reaction product and the excess air and ammonia through a heat exchanger to cool said air and ammonia and thereby cool the ammonium phosphate suspended therein, passing said ammonium phos-' phate reaction product while in suspension in said excess air to a collector containing air pervious filter surfaces, varying the relative rates of feed of phosphorus, and air, measuring the temperature of'the air and gas stream with its entrained ammonium phosphate as it leaves the heat exchanger, determining the temperature of said stream at which the filter surfaces of said collector become plugged by the conver-'- sion of said ammonium phosphate powder to a sticky glass-like material, and regulatin the relative rates of supply of phosphorus and air to said chamber to such a value that the temperature of the air andphosphate product as it leaves the heat exchanger is below the value at which plugging of the filter surfaces occurs. 11. A method of producin ammonium phosphate as a dry crystalline product having a composition corresponding substantially to the formula NHiPOs comprising supplying phosphorus and atmospheric air containing moisture to a combustion chamber, so regulating the amount of air supplied relative to the amount of phosphorus supplied that there is a substantial excess of air over the amount required to effect both a conversion of the phosphorus to phosphorus pentoxide and cooling of the phosphorus pentoxide to a temperature between about 900 F. and 600 F. introducing ammonia-into the combustion chamber in amount in excess of the theoretical amount required to react with phosphorus pentoxide and water vapor to form Nl-LlPOz continuously removing the reaction product, excess air and ammonia from the combustion chamber, and cooling the ammonium phosphate product from the temperature at which it is formed to a temperature below about 400 F. to 450 F. at such a rate that the product does not decompose to a sticky substance, and collecting said ammonium phosphate product by passing the same through filters.

12. A method according to claim 11 characterized by the fact that the ammonia and elemental phosphorus are supplied at such rates that the ratio of ammonia to phosphorus is between about 1.25:1 to about 2:1 on a weight basis,

13. A method according to claim 11 characterized by the fact that water as such is supplied to the combustion chamber in amount sufficient to compensate for deficiency of moisture in the atmospheric air supplied to said chamber and required for the reaction resulting in NH4PO3.

14. A process of producing crystalline ammonium metaphosphate as a free-flowing powder by gas phase reaction between water vapor, gaseous phosphorus pentoxide and ammonia gas that consists in continuously supplying molten elemental phosphorus and atmospheric air containing moisture to a combustion chamber at such rates relative to each other, that the phosphorus is burned to gaseous phosphorus pentoxide, cooling the water vapor and the gaseous phosphorus pentoxide formed in said combustion chamber by introducing air into the same at such a rate as to maintain the temperature in said combustion chamber withina range of about 600 F. to about 900 F., continuously introducing ammonia gas into said cooled gaseous phosphorus pentoxide and Water vapor at a rate sufficient to effect a gas phase reaction of the ammonia and the water vapor with all of the gaseous phosphorus pentoxide at the rate at which it is formed in said chamber to form ammonium metaphosphate, continuously removin the ammonium metaphosphate and excess air in which it is entrained from the reaction zone and cooling the same from the temperature existing at the. time of said reaction to a temperature of about 400% F. to 450 F. in a period of time not exceeding about eight seconds measured from about the instant the ammonium metaphosphate is formed in said gas phase reaction, separating said crystalline ammonium metaphosphate powder from the excess air and ammonia and collecting the same in a collector.

15. A process of producing crystalline ammonium metaphosphate as a free-flowing powder by gas phase reaction between Water vapor, gaseous phosphorus pentoxide and ammonia gas that consists in continuously supplyin molten elemental phosphorus and atmospheric air containing moisture to a combustion chamber at such rates relative to each other, that the phosphorus is burned to gaseous phosphorus pentoxide, cooling the water vapor and the gaseous phosphorus pentoxide formed in said combustion chamber by introducing air into the same at such a rate as to maintain the temperature in said combustion chamber within a range above about 600 F.

and below the temperature at which ammonia gas monium metaphosphate, continuously removing the ammonium metaphosphate and excess air in which it is entrained from the reaction zone and cooling the same from the temperature existing at the time of said reaction to a temperature of about 400 F. to 450 F. in a period of time not exceeding about eight seconds measured from about the instant the ammonium metaphosphate isformed in said gas phase reaction, separating said crystalline ammonium metaphosphate pow der from the excess air and ammonia and collecting the same in a collector.

16. A process of producing crystalline ammonium metaphosphate as a free-flowing powder by gas phase reaction between water vapor, gaseous phosphorus pentoxide and ammonia gas that consists in continuously supplying molten elemental phosphorus and atmospheric air containing moisture to a combustion chamber at such rates relative to each other, that the phosphorus is burned to gaseous phosphorus pentoxide, cooling the water vapor and the gaseous phosphorus pentoxide formed in said combustion chamber by introducing air into the same at such a rate as to maintain the temperature in said combustion chamber within a range of about 600 F to about 900 F., continuously introducin ammonia gas into said cooled gaseous phosphorus pentoxide and water vapor at a rate suflicient to eifect a gas phase reaction of the ammonia and the Water vapor with all of the gaseous phosphorus pentoxide at the rate at which it is formed in said chamber to form ammonium metaphosphate, continuously removing the ammonium metaphosphate and excess air in which it is entrained from the reaction zone and cooling the same from the temperature existing at the time of said reaction to a temperature of about 400 F. to 450 F. in a period of time not exceeding about eight seconds measured from about the instant the ammonium metaphosphate is formed in said gas phase reaction, and passing the cooled air and the entrained ammonium metaphosphate through air-pervious filters whereby the ammo nium metaphosphate is separated from said air' and collected. Y

OWEN RICE.

REFERENCES CITED The following references are of record in the file of this patent:

UNITED STATES PATENTS Number Name Date 1,194,077 Ross et al. Aug. 8, 1916 1,514,912 Klugh Nov. 11, 1924 2,142,943 Kerschbaum Jan. 3, 1939' 2,280,848 Pole Apr. 28, 1942 

1. A METHOF OF PRODUCING AMMONIUM METAPHOSPHATE AS A DRY FREE-FLOWING POWDER THAT CONSISTS IN SUPPLYING AIR CONTAINING MOISTURE AND ELEMENTAL PHOSPHORUS TO A COMBUSTION CHAMBER AT SUCH RATIOS RELATIVE TO EACH OTHER THAT THE PHOSPHORUS IS BURNED TO GASEOUS PHOSPHORUS PENTOXIDE AND SUPPLYING THE PHOSPHORUS AND AIR TO SAID COMBUSTION DEVELOPED IN SAID CHAMBER BY THE TEMPERATUE CHAMBER IN SAID CHAMBER BY SAID COMBUSTION IS ABOVE 600* F., INTRODUCING AMMONIA INTO THE PHOSPHORUS PENTOXIDE FORMED IN SAID CHAMBER AND THE WATER VAPOR MIXED THEREWITH IN SUCH AMOUNT THAT THE AMMONIA AND WATER VAPOR REACT WITH ALL THE GASEOUS PHOSPHORUS PENTOXIDE TO FORM AMMONIUM METAPHOSPHATE WHILE THE REACTANTS ARE IN THE GAS PHASE, CONTINUOUSLY DISCHARGING THE EXCESS AIR AND AMMONIUM METAPHOSPHATE SO FORMED INTO A FILTER, AND COOLING THE AMMONIUM METAPHOSPHATE AND 